Apparatus and method for controlling an ammonia production system

ABSTRACT

An apparatus, method, and computer program for controlling an ammonia production system are provided. At least one model is associated with production equipment operable to produce ammonia, where the production equipment includes a reformer section, a carbon dioxide wash section, and an ammonia synthesis reactor section. The production equipment is controlled using the at least one model. The at least one model is associated with a plurality of controlled variables and a plurality of manipulated variables. At least some of the controlled variables are associated with the reformer section, the carbon dioxide wash section, and/or the ammonia synthesis reactor section. At least some of the manipulated variables are associated with the reformer section, the carbon dioxide wash section, and/or the ammonia synthesis reactor section.

TECHNICAL FIELD

This disclosure relates generally to control systems and morespecifically to an apparatus and method for controlling an ammoniaproduction system.

BACKGROUND

An ammonia production plant typically includes a complex arrangement ofequipment designed to convert natural gas into ammonia. Often times, thenatural gas is used as both a raw material to produce ammonia and as afuel for the equipment in the production plant. Ideally, the ammoniaproduction plant is operated such that the production of ammonia ismaximized while the consumption of natural gas and energy is minimized.However, conventional control systems are typically unable to meet thesecontrol and optimization objectives given the numerous constraints oftenassociated with these objectives.

SUMMARY

This disclosure provides an apparatus and method for controlling anammonia production system.

In a first embodiment, an apparatus includes at least one memoryoperable to store at least one model. The at least one model isassociated with production equipment operable to produce ammonia. Theproduction equipment includes a reformer section, a carbon dioxide washsection, and an ammonia synthesis reactor section. The apparatus alsoincludes at least one processor operable to control the productionequipment using the at least one model. The at least one model isassociated with a plurality of controlled variables and a plurality ofmanipulated variables. At least some of the controlled variables areassociated with at least one of: the reformer section, the carbondioxide wash section, and the ammonia synthesis reactor section. Atleast some of the manipulated variables are associated with at least oneof: the reformer section, the carbon dioxide wash section, and theammonia synthesis reactor section.

In particular embodiments, the reformer section includes a primaryreformer and a secondary reformer. Also, at least one of the controlledvariables is associated with at least one of: methane slip in thesecondary reformer, an air compressor that is operable to affectoperation of the reformer section, and one or more heating limits of theprimary reformer. In addition, at least one of the manipulated variablesis associated with at least one of: a natural gas feed flow, a steamflow or steam-to-gas ratio or steam-to-hydrocarbon ratio in the primaryreformer, an air flow or air-to-gas ratio in the secondary reformer, andmethane slip in the primary reformer.

In other particular embodiments, at least one of the controlledvariables is associated with carbon dioxide slip in the carbon dioxidewash section. Also, at least one of the manipulated variables isassociated with at least one of: a flow rate of a lean solution in thecarbon dioxide wash section, and a temperature of the lean solution.

In yet other particular embodiments, at least one of the controlledvariables is associated with at least one of: a pressure of a synthesisreactor in the ammonia synthesis reactor section, and a synthesis gascompressor in the ammonia synthesis reactor section. Also, at least oneof the manipulated variables is associated with a suction pressure ofthe synthesis gas compressor.

In a second embodiment, a method includes storing at least one model,where the at least one model is associated with production equipmentoperable to produce ammonia. The production equipment includes areformer section, a carbon dioxide wash section, and an ammoniasynthesis reactor section. The method also includes controlling theproduction equipment using the at least one model. The at least onemodel is associated with a plurality of controlled variables and aplurality of manipulated variables. At least some of the controlledvariables are associated with at least one of: the reformer section, thecarbon dioxide wash section, and the ammonia synthesis reactor section.At least some of the manipulated variables are associated with at leastone of: the reformer section, the carbon dioxide wash section, and theammonia synthesis reactor section.

In a third embodiment, a computer program is embodied on a computerreadable medium and is operable to be executed by a processor. Thecomputer program includes computer readable program code for storing atleast one model that is associated with production equipment operable toproduce ammonia. The production equipment includes a reformer section, acarbon dioxide wash section, and an ammonia synthesis reactor section.The computer program also includes computer readable program code forcontrolling the production equipment using the at least one model. Theat least one model is associated with a plurality of controlledvariables and a plurality of manipulated variables. At least some of thecontrolled variables are associated with at least one of: the reformersection, the carbon dioxide wash section, and the ammonia synthesisreactor section. At least some of the manipulated variables areassociated with at least one of: the reformer section, the carbondioxide wash section, and the ammonia synthesis reactor section.

Other technical features may be readily apparent to one skilled in theart from the following figures, descriptions, and claims.

BRIEF DESCRIPTION OF THE DRAWINGS

For a more complete understanding of this disclosure, reference is nowmade to the following description, taken in conjunction with theaccompanying drawings, in which:

FIG. 1 illustrates an example ammonia production system;

FIGS. 2A through 2I illustrate example models for controlling an ammoniaproduction system;

FIGS. 3A through 3I illustrate an example user interface for controllingan ammonia production system; and

FIG. 4 illustrates an example method for controlling an ammoniaproduction system.

DETAILED DESCRIPTION

FIG. 1 illustrates an example ammonia production system 100. Theembodiment of the ammonia production system 100 shown in FIG. 1 is forillustration only. Other embodiments of the ammonia production system100 may be used without departing from the scope of this disclosure.

In this example embodiment, the ammonia production system 100 includesproduction equipment 102 for processing natural gas received through apipeline 104 to produce ammonia. An advanced process control (APC)system 106 controls the production equipment 102 to increase or maximizethe production of ammonia while reducing or minimizing the use of fuelor energy by the production equipment 102 (such as natural gas used asfuel by the production equipment 102).

As shown in FIG. 1, the production equipment 102 includes variouscomponents for processing natural gas to produce ammonia. The productionequipment 102 (shown in simplified form) in this example embodimentrepresents a Braun Purifier-type ammonia production system. Thefollowing details represent a specific implementation of the productionequipment 102 in the ammonia production system 100. Other embodiments ofthe ammonia production system 100 could be used.

Feedstocks provided to the production equipment 102 include natural gas,ambient air, and water. The natural gas enters via the pipeline 104. Thecomposition of the natural gas may fluctuate in methane (CH₄) content,which can be seen as density fluctuations. The gas might normallycontain approximately 98% methane, but this could drop to approximately95% methane. The consumption of natural gas by the production equipment102 during normal operation could be approximately 689 normal cubicmeters (Nm³) of natural gas per ton of ammonia produced. Among otherthings, the natural gas can be used as a raw material to produce theammonia. The natural gas can also be used as a fuel for one or more gasturbines 108, which can be used to drive one or more air compressors110. The natural gas can also be used as fuel for one or more gasburners 118 of a primary reformer 116.

In this particular embodiment, natural gas is desulphurized in a gashydrotreater 114. The natural gas is also mixed with steam to feed theprimary reformer 116. In heated catalyst tubes of the primary reformer116, the methane reacts with water to produce carbon monoxide andhydrogen gas (the endothermic reaction CH₄+H₂O<->CO+3H₂). Combustion airfor the burners 118 in the primary reformer 116 is hot exhaust gas fromthe gas turbine 108, allowing combustion heat to be recovered. Here, thegas burners 118 may include side burners that heat the catalyst tubesand an auxiliary burner used to generate heat for steam production.

The primary reformer effluent is fed to a secondary reformer 120, whereit is mixed with compressed air. In a catalyst bed in the secondaryreformer 120, methane reacts with oxygen gas to produce carbon monoxideand hydrogen gas (the exothermic reaction 2CH₄+O₂<->2CO+4H₂). The airused here could be ambient air.

Water is vaporized to produce steam in one or more heat exchangers 112,which quench the secondary reformer effluent. This steam is superheatedin a convection section of the primary reformer 116. More heat isrecovered from the primary reformer convection by preheating processfeed gas, boiler water, and air provided to the secondary reformer.

The quenched secondary reformer effluent is sent to a high temperatureshift reactor and a low temperature shift reactor (generally referred toas shift reactors 122). In catalyst beds in the shift reactors 122, thecarbon monoxide reacts with water to produce carbon dioxide and hydrogengas (the reaction CO+H₂O<->CO₂+H₂). The carbon dioxide is removed in acarbon dioxide wash column 124, where the carbon dioxide is absorbed inan aqueous methyldiethanolamine (MDEA) solution. Since carbon dioxide isa catalyst poison for ammonia synthesis, any carbon monoxide and carbondioxide slip from the wash column 124 is converted to methane in amethanizer 126 (according to the exothermic reactions CO+3H₂->CH₄+H₂Oand CO₂+4H₂->CH₄+2H₂O).

The water is removed in one or more dryers 128, and the resulting gas isfed to one or more purifiers 130. In the purifiers 130, most or allmethane and a large part of any neon and argon traces are washed out viacontact with liquid nitrogen. The purifier effluent is synthesis gasformed of nitrogen (from ambient air) and hydrogen. The ratio ofnitrogen to hydrogen may be controlled by liquid nitrogen reflux in thepurifier 130. The gas removed in the purifier 130 can be used as fuelgas in the primary reformer 116.

The synthesis gas is compressed by a synthesis gas compressor 134, whichis driven by multiple steam turbines 132 on a single shaft. In twosynthesis reactors 136, the synthesis gas is converted to ammonia incatalyst beds (according to the reaction N₂+3H₂<->2NH₃). The synthesisreactor ammonia effluent is cooled against boiler water, generating highpressure steam. The reactor effluent can be further cooled againstprocess streams to recover heat, and the ammonia is condensed in anammonia refridge system 138 driven by an ammonia compressor 140. Therest of the gas is recycled to the synthesis gas compressor 134. A smallpurge flow can be used to prevent and control accumulation of inertgasses such as argon. This purge gas may be sent back to the purifierfeed so that no hydrogen is lost. This means that the only route out forinert gasses such as argon is via the purifier off gas to the primaryreformer fuel gas. The methane content of the purifier off gas can becontrolled by injecting a small flow of fresh natural gas.

The superheated high pressure steam drives the steam turbines 132, whichdrive the synthesis gas compressor 134. In particular embodiments, onesteam turbine (denoted HD1) could reduce the steam pressure to mediumpressure and control this pressure, where the medium pressure steam isused with the production equipment 102. Another steam turbine (denotedHD2) could reduce the pressure to low pressure and deliver the steam toa low pressure steam header, and this turbine could control the highpressure steam pressure. The speed of the synthesis gas compressor 134may be controlled by a third turbine (denoted ND) on the same shaft thatis fed with steam from the low pressure steam header. The thirdturbine's back pressure may be controlled by a steam condenser. Themedium pressure steam is used as a reactant in the primary reformer 116,and surplus steam is delivered to the low pressure steam header.

As noted above, the APC system 106 may control the production equipment102 to increase or maximize the production of ammonia while reducing orminimizing the use of fuel or energy by the production equipment 102.The APC system 106 could, for example, increase or maximize ammoniaproduction by reducing the variability of key control parameters andsetting appropriate control targets closer to their limits. This couldbe done with a built-in optimizer that maximizes throughput while takinginto consideration the specifications for the system 100 and thespecifications for the product (ammonia) being produced. The APC system106 could reduce or minimize natural gas or energy consumption byoptimizing any remaining degrees of freedom subject to certainconstraints. The optimization of the remaining degrees of freedom may bedone using an economic objective function that maximizes plant profit.In particular embodiments, the APC system 106 controls the primaryreformer 116, secondary reformer 120, wash column 124, and synthesisreactors 136 to increase or maximize ammonia production and reduce orminimize natural gas or energy consumption.

The APC system 106 represents any hardware, software, firmware, orcombination thereof for controlling the production equipment 102. TheAPC system 106 could, for example, include one or more processors 142and one or more memories 144 storing data and instructions (such asmodels of the system 100) used or generated by the processor(s) 142. Asa particular example, the APC system 106 could represent a controllerimplemented using Robust Multivariable Predictive Control Technology(RMPCT) supporting multivariable predictive constraint and optimizationcontrol, which could be implemented as a software package 146. Thesoftware package 146 could, for example, be executed in the WINDOWS 2000operating system at a fifteen second frequency on a TPS APP NODE fromHONEYWELL INTERNATIONAL INC. The APC system 106 could include variouscontrollers used to control different aspects of the productionequipment 102.

Additional details regarding the operations and controls provided by theAPC system 106 follow. These details represent possible implementationsof the APC system 106 only. They are provided simply as examples of howthe APC system 106 can control the production equipment 102.

In general, the system 100 is associated with various “processvariables,” which represent various aspects of the system 100 (such asflow rate, pressure, or volume). The APC system 106 may operate byattempting to maintain a “controlled” process variable at or near adesired value or within a desired operating range. The APC system 106attempts to maintain the controlled variable by altering one or more“manipulated” process variables (such as an opening of a valve or aspeed of a turbine). A “disturbance” variable represents a processvariable that affects a controlled variable, where the disturbancevariable can be considered by the APC system 106 when altering themanipulated variables but generally cannot be controlled by the APCsystem 106 (such as ambient temperature). By controlling certaincontrolled variables, the APC system 106 may reduce the variability ofthe controlled variables and set the controlled variables closer totheir limits, thereby increasing or maximizing ammonia production.

To reduce or minimize natural gas or energy consumption, the APC system106 could be configured with linear program (LP) economics or quadraticprogram (QP) economics that maximize plant profit. These two differenteconomic optimization approaches use a minimization strategy, and thequadratic optimization can also use ideal resting values (or desiredsteady state values). The general form of an objective function couldbe:

${{Minimize}\mspace{14mu} J} = {{\sum\limits_{i}{b_{i} \times {CV}_{i}}} + {\sum\limits_{i}{a_{i}^{2}\left( {{CV}_{i} - {CV}_{0i}} \right)}^{2}} + {\sum\limits_{j}{b_{j} \times {MV}_{j}}} + {\sum\limits_{j}{a_{j}^{2}\left( {{MV}_{j} - {MV}_{0j}} \right)}^{2}}}$

where:

b_(i) represents the linear coefficient of the i^(th) controlledvariable;

b_(j) represents the linear coefficient of the j^(th) manipulatedvariable;

a_(i) represents the quadratic coefficient of the i^(th) controlledvariable;

a_(j) represents the quadratic coefficient of the j^(th) manipulatedvariable;

CV_(i) represents the actual resting value of the i^(th) controlledvariable;

CV_(0i) represents the desired resting value of the i^(th) controlledvariable;

MV_(j) represents the actual resting value of the j^(th) manipulatedvariable; and

MV_(0j) represents the desired resting value of the j^(th) manipulatedvariable.

As shown here, the optimization may involve a large number of processvariables, each able to be incorporated into either a linear orquadratic optimization objective. The APC system 106 can optimize thecontrolled variables (once ammonia production is increased or maximized)using this optimization to reduce fuel/energy consumption.

These represent general approaches as to how the APC system 106 canincrease or maximize ammonia production and decrease or minimizefuel/energy consumption. The following represents additional details ofhow these operations could be performed by the APC system 106. Again,these details describe example operations only. In the followingdiscussion, various operations of the production equipment 102 aredescribed, followed by an explanation as to how certain processvariables can be controlled by the APC system 106.

In the convection section of the primary reformer 116, water may besprayed into the superheated steam to control the temperature at about450° C. A master controller may control the steam temperature, and awater injection flow controller may act as a slave. If more fuel gas issent to the auxiliary gas burner 118 in the primary reformer 116, thesteam temperature controller may inject more water to maintain thetemperature, which produces more high pressure steam.

The air flow to the secondary reformer 120 may be measured andcontrolled by an air flow controller manipulating a gas turbine speedcontroller setpoint. An air/gas ratio controller can be used to send asetpoint to the air flow controller. Similarly, a steam/gas ratiocontroller may manipulate a steam-to-primary reformer flow controllersetpoint.

In order to maximize ammonia production, the APC system 106 may supporta single Robust Multivariable Predictive Control (RMPCT) strategy. TheAPC system 106 may solve the entire control problem simultaneously andbe executed at a fifteen-second frequency.

The design of the APC system 106 can be as follows. Controlled variablesused by the APC system 106 are listed in Table 1. The “Critical” columnindicates the controlled variables that are set as critical in the APCsystem 106.

TABLE 1 Controlled Variables Name Critical CH₄ slip secondary reformer(process CV1 variable) CO₂ slip treated gas (process variable) CV2Calculated variable: Inlet Guide Vanes CV3 gas turbine & exhausttemperature gas turbine difference (compressor limits) Pressure safetyvalves (process CV4 C variable) Delta pressure air combination (processCV5 variable) Stack gas dampers (primary reformer CV6 C heating limit)(output variable) HP steam quench valve positions (high CV7 select)(primary reformer heating limit) (output variable) ND turbine valveposition (synthesis CV8 C gas compressor limit) HD2 turbine valveposition (synthesis CV9 C gas compressor limit) Synthesis reactorpressure (process CV10 C variable) Natural gas flow controller outputCV11 (output variable) Steam flow controller output (output CV12variable) Air flow controller output (output CV13 variable) CO₂ washbottom level controller output CV14 (output variable)

Each of these controlled variables could have validation limits, such aswhen each controlled variable is validated against a high value, a lowvalue, a rate of change, and a frozen value. Table 2 shows the followingfor each of the controlled variables: absolute high and low limits, rateof change limit, and freeze tolerance and time. A controlled variablemay be flagged as being bad if one of its limits is exceeded. Also, if acontrolled variable changes less than the freeze tolerance during thefreeze time window, it may represent a frozen value and be flagged asbeing bad.

TABLE 2 Freeze Name Description High Low Roc/exec tolerance Freezeminutes CV1 CH₄ slip secondary 2 1 0.25 0.0001 5 reformer CV2 CO₂ sliptreated gas 2000 −1 2000 — — CV3 Inlet Guide Vanes 100 −1 5 0.001 5 gasturbine & exhaust temperature gas turbine difference CV4 Pressure safety32 20 10 0.0005 5 valves CV5 Delta pressure air 2.5 0.25 2.5 0.0005 5combination CV10 Synthesis reactor 210 100 100 0.0001 5 pressure CV8 NDturbine valve 280 0 280 0 5 position CV9 HD2 turbine valve 280 0 280 0 5positionHere, ROC/exec refers to the rate of change per execution. To determineROC/minute (the rate of change per minute), multiply the value in Table2 by four (since the execution time is 15 seconds). Also, the CO₂ slipmay have no freeze detection because it can be “frozen” at zero for longperiods of time without any associated instrument malfunction.

The manipulated variables used by the APC system 106 to control thesecontrolled variables are listed in Table 3. In this example, nomanipulated variables are set as critical in the APC system 106,although various ones of the manipulated variables could be.

TABLE 3 Manipulated Variables Name Natural gas feed flow rate MV1Primary reformer Steam-to-Gas or Steam-to-Hydrocarbon MV2 (S/H) molratio Secondary reformer Air-to-Gas (A/G) normal volume ratio MV3Primary reformer methane slip MV4 Fuel gas flow rate to auxiliaryburners MV5 Lean solution to wash column flow rate MV6 Semi leansolution flow rate MV7 Lean solution to wash column temperature MV8Synthesis gas compressor suction pressure MV9The process variables treated as disturbance variables by the APC system106 during the control of the controlled variables are listed in Table4.

TABLE 4 Disturbance Variables Name Ambient Temperature DV1 Compositionnatural gas DV2 Lean solution PV temperature DV3The lean solution PV temperature may be representative of externaldisturbances, such as ambient temperature or watering coolers. Theambient temperature itself can be used for feed forward of airtemperature-density effects on the gas turbine 108. It may or may not beuseful to use the natural gas composition as feed forward, and thisdisturbance variable could be included for use if desired.

By controlling the controlled variables using these manipulatedvariables and disturbance variables, the APC system 106 may moreeffectively manage the production equipment 102, helping to increase ormaximize ammonia production in the system 100. For example, the APCsystem 106 may use various models associating specified controlledvariables to specified manipulated or disturbance variables to controlthe production equipment 102.

As noted above, the APC system 106 may reduce the variability of keycontrol parameters and set appropriate control targets closer to theirlimits, while reducing or minimizing fuel/energy consumption byoptimizing any remaining degrees of freedom subject to certainconstraints. This may be done with a built-in optimizer in the APCsystem 106. Table 5 identifies variables that may have a linear program(LP) coefficient unequal to zero in the minimization objective function.

TABLE 5 LP Variable Name Coefficicient Objective MV: Natural gas flowMV1 −20 Maximize CV: CO₂ slip CV2 0.1 Minimize MV: Lean solution MV6−0.1 MaximizeThe CO₂ slip variable may have a value between two constraints (such as150-300 ppm). Also, while shown as maximizing the natural gas flow andthe lean solution, this may also result in a small energy saving.Similarly, Table 6 identifies variables that may have a quadraticprogram (QP) coefficient unequal to zero in the minimization objectivefunction and that can be optimized to example desired values.

TABLE 6 QP Variable Name Coefficicient Desired value CV: Methane slip2^(nd) CV1 0.1 1.5 reformer MV: Syn gas compressor MV9 0.01 22.2 suctionpressureBy minimizing the objective function shown above with this information,the APC system 106 may more effectively manage the production equipment102, helping to reduce or minimize fuel/energy consumption in the system100.

In some embodiments, the APC system 106 may use MV1-MV4 to control CV1,CV3, CV6, and CV7. The APC system 106 may operate using the followingcontrol objectives: keep CV1 between specified limits, keep CV3 belowthe compressor's operating limit, and keep CV6 and CV7 below theirheating limits. Once these control objectives are accomplished, thefollowing optimization objectives can be implemented: maximize plantthroughput subject to limits in all sections of the plant, maintain CV1at an optimum target to minimize natural gas consumption, and maintainMV4 as close as possible to an optimum target to minimize natural gasconsumption.

Similarly, the APC system 106 may use MV6 and optionally MV8 to controlCV2. The APC system 106 may operate using the following controlobjective: keep CV2 below its maximum limit. Once this control objectiveis accomplished, the following optimization objectives can beimplemented: minimize CV2 to a low limit, and minimize MV6 subject toCV2 limit to save energy.

In addition, the APC system 106 may use MV9 to control CV8-CV10. The APCsystem 106 may operate using the following control objectives: keep CV10below its maximum limit, and keep CV8 and CV9 below their operatinglimits. Once these control objectives are accomplished, the followingoptimization objective can be implemented: maintain MV9 as close aspossible to an optimum target.

As noted above, calculated variables can be used during the control ofthe production equipment 102. For example, the value of CV3 could becalculated as follows:

CV3=−2.1*Gas turbine inlet guide vane position+Gas turbine exhausttemperature difference+172.3.

Using the controlled, manipulated, and disturbance variables definedabove in the various tables, models can be constructed of the ammoniaproduction system 100. These models could be generated, for example,using step-test data involving various production equipment 102. Table 7identifies example model relationships between various ones of thecontrolled, manipulated, and disturbance variables. In Table 7, a “+”entry indicates a positive gain, a “−” entry indicates a negative gain,and a blank entry indicates no model (no relationship) is used.

TABLE 7 MV/DV CV MV1 MV2 MV3 MV4 MV5 MV6 MV7 MV8 MV9 DV1 DV2 DV3 CV1 −− + CV2 + + − − + + CV3 − − − CV4 + + + CV5 + + − + CV6 + + + CV7 + −− + + CV8 + − − − CV9 + − + − + CV10 + + + CV11 + + + CV12 + + +CV13 + + + + CV14 + +Actual models defining example relationships between various ones of thecontrolled, manipulated, and disturbance variables are shown in FIGS. 2Athrough 2I. In these figures, blank entries represent null transferfunctions, meaning no model is used in the APC system 106. Using themodels shown in FIGS. 2A through 2I, the APC system 106 can effectivelyincrease or maximize ammonia production while reducing or decreasingfuel/energy consumption. For example, the models shown in FIGS. 2Athrough 2I may allow the APC system 106 to determine how to makeadjustments to the manipulated variables to help the controlledvariables reach desired operating values or ranges while reducingvariability and setting the controlled variables' targets closer totheir limits.

FIGS. 3A through 3I illustrate an example user interface 300 that can beused or supported by the APC system 106. The user interface 300 may, forexample, allow a user to tune the APC system 106 or perform variousother functions. In this example, the user interface 300 includescontrol buttons 302, which allow the user to invoke various high-levelfunctions related to the APC system 106. In this example, the controlbuttons 302 allow the user to place the APC system 106 in an on, off, orwarm state. The control buttons 302 also allow the user to view anapplication menu, set various high-level options, and view statusmessages or reports.

When the APC system 106 is activated using the appropriate controlbutton 302, function buttons 304 can be used to invoke particularfunctions by the user or to display particular information to the user.The information could, for example, be displayed in a display area 306of the user interface 300. As shown in FIG. 3A, selection of the “CVOptimize” button 304 allows the user to view and configure the optimizeras it relates to the controlled variables. For each controlled variable,the display area 306 includes a numerical index and a tag name. Thedisplay area 306 also includes LP and QP coefficient values and adesired QP coefficient value, which can be used to set the appropriateeconomic objectives for the controlled variable. The display area 306further includes delta soft low and high values representingoptimization soft limits and an error tolerance representing how far thecontrolled variable can exceed its soft limits to permit optimization.The user can review the data associated with the controlled variablesand make modifications to this data as desired.

As shown in FIG. 3B, selection of the “MV Optimize” button 304 allowsthe user to view and configure the optimizer as it relates to themanipulated variables. For each manipulated variable, the display area306 includes a numerical index, a tag name, LP and QP coefficientvalues, a desired QP coefficient value, and delta soft low and highvalues. The user can review the data associated with the manipulatedvariables and make modifications to this data as desired.

As shown in FIG. 3C, selection of the “CV Control” button 304 allows theuser to view and make tuning changes for controlling the controlledvariables. For each controlled variable, the display area 306 includes anumerical index and a tag name. A performance ratio identifies how hardthe controller pushes the controlled variable back to its setpoint oraway from a limit violation. A closed loop response interval identifiesthe response time for pushing the controlled variable back to itssetpoint or away from a limit violation. Low and high “EU Give Up”values identify a priority of the controlled variable, which can be usedwhen the APC system 106 is unable to keep all controlled variables attheir setpoints or away from their limits. A number of blocks identifiesthe number of times that the APC system 106 makes a prediction for thecontrolled variable during the closed loop response interval. A feedforward (FF) to feedback (FB) performance ratio identifies howaggressively the APC system 106 rejects disturbance variabledisturbances. A state estimation is used to control the correction ofbias and ramp rates.

As shown in FIG. 3D, selection of the “MV Control” button 304 allows theuser to view and make tuning changes for controlling the manipulatedvariables. For each manipulated variable, the display area 306 includesa numerical index and a tag name. A number of blocks identifies thenumber of times that the APC system 106 computes movements for themanipulated variable during a period of time. Maximum move down and moveup values represent the largest changes that can be made to themanipulated variable at each execution. A weight represents a penaltyassociated with moving one manipulated variable relative to othermanipulated variables. A predict back (PB) or setpoint tracking (SPTR)ratio identifies how fast the APC system 106 adjusts a setpoint toaddress manipulated variable windup.

As shown in FIG. 3E, selection of the “CV Process” button 304 allows theuser to view and make changes to the controlled variables. For eachcontrolled variable, the display area 306 includes a numerical index, atag name, and low and high ramp limits that control how fast activelimits ramp or change to meet new values. A number of bad reads valueidentifies the number of bad values that is acceptable for a controlledvariable. A PV value compensation ratio identifies the amount of acorrective signal that can be subtracted from an input signal, which isuseful in cases where a controlled variable naturally oscillates. Atrack limits value can be used to prevent the APC system 106 from makingchanges to manipulated variables when the controlled variable is beinginitialized. A critical value indicates whether the controlled variableis critical, and an update frequency indicates whether the controlledvariable is updated at least once per execution.

As shown in FIG. 3F, selection of the “MV Process” button 304 allows theuser to view and make changes to the manipulated variables. For eachmanipulated variable, the display area 306 includes a numerical index, atag name, low and high ramp limits, and a critical value. A track limitsvalue controls whether the APC system 106 attempts to move themanipulated variable when it is outside its limits duringinitialization. A manual value indicates whether the manipulatedvariable is dropped or used as a feed forward value when the manipulatedvariable is not available for control.

As shown in FIG. 3G, selection of the “CV Advanced Tuning” button 304allows the user to view and make advanced tuning changes for controllingthe controlled variables. For each controlled variable, the display area306 includes a numerical index, a tag name, and a closed loop responseinterval. If a controlled variable involves the use of an integrator, anintegrator balance factor can be specified, and a hold integrator valuesets the behavior when an infeasibility occurs. A balance targetidentifies the steady-state horizon for optimization in intervals. Afunnel type identifies a funnel shape for controlling dynamicexcursions, and a decouple ratio value can be used in conjunction withcertain funnel type(s).

As shown in FIG. 3H, selection of the “Controller Detail” button 302presents general information about the APC system 106 (the controller)to the user. This can include information associated with the modelsused by the APC system 106 to control the production equipment 102. Itcan also include high-level information about variables associated withthe model and the current performance of the controller.

As shown in FIG. 3I, a toolkit can be provided to support the RMPCTfunctionality described above. The RMPCT tbolkit could, for example, beimplemented and configured on the same APP NODE with PROFIT CONTROLLERsoftware from HONEYWELL INTERNATIONAL INC. The toolkit may containvarious functions, such as functions used for controlled variablevalidation purposes as described above with respect to Table 2. TheROC/exec, freeze tolerance, and freeze minutes could be configured here.These functions are denoted ASynCV01 through ASynCV10 (asynchronouscontrolled variable validation) in this example.

Other functions supported by the toolkit could include functions forautomating actions related to manipulated variables being dropped orused as a feed forward value (when the manipulated variables are notavailable for control as described above). These functions are denotedFF_OFF_MAN1 through FF_OFF_MAN9 in this example. Some specific examplesof these functions are as follows. Assume the APC system 106 is on withsome manipulated variables set to OPR (manual mode of operation) and astatus set to FFWD (feed forward), and downstream controllers for thesemanipulated variables are in AUTO (automatic) mode.

If an operator changes the mode of a downstream controller (for aparticular manipulated variable) from automatic to manual, the toolkitsets the feed forward flag of that particular manipulated variable tooff. This means the controller does not use this manipulated variable(the manipulated variable has a status of SERV, meaning communicationhas been lost).

If an operator takes the downstream controller (for a particularmanipulated variable) back in automatic mode from manual mode, the feedforward flag of that manipulated variable is set to on, and thecontroller uses this manipulated variable (its status is FFWD).

For the manipulated variables that implement a ratio controller (such asMV2 & MV3), the reasoning above holds if either of the two underlyingdownstream controllers belonging to the same manipulated variable istaken from automatic mode to manual mode and vice-versa.

Alternative to the above, the default behaviour may be to have thestatus equal FFWD for the manipulated variables regardless of whetherthe downstream controller is in automatic or manual mode.

Additional operations can also occur in the APC system 106. For example,if the mode of a downstream controller for a manipulated variable ischanged from cascade to automatic, the APC system 106 may shut itselfoff as a default behaviour. Also, the APC system 106 may send messagesboth to an LCN message summary and journal, as well as to an RMPCTjournal summary. In addition, administrative rights can be enforced inthe APC system 106, such as when only “administrators” can change rightsor access the “Options” button 302. Example access rights can be definedas follows for operators and engineers:

RMPCT WARM BUTTON FOR SS INITIALIZATION OPER1 CV AND MV OPERATOR LIMITRAMP RATES ENGR CV AND MV DESIRED OPT TARGET VALUES ENGR MV FEEDFORWARD/SERVICE SWITCH ENGR CV ENGINEERING HIGH/LOW HARD LIMITS ENGR MVENGINEERING HIGH/LOW HARD LIMITS ENGR.

In particular embodiments, the APC system 106 can be implemented usingPROFIT CONTROLLER from HONEYWELL INTERNATIONAL INC. on an APP NODErunning WINDOWS 2000. For displaying APC information, PROFIT VIEWER canbe used on GUS STATIONS in a control room, or standard PROFIT CONTROLLERnative window displays can be used. PROFIT VIEWER can also be used on astandard computing device made part of the appropriate TPS domain.Computers with PROFIT VIEWER installed can communicate with the APP NODEusing OPC.

Although FIG. 1 illustrates one example of an ammonia production system100, various changes could be made to FIG. 1. For example, other oradditional production equipment 102 could be used in any suitableconfiguration or arrangement to produce ammonia. Although FIGS. 2Athrough 2I illustrate examples of models for controlling an ammoniaproduction system, any other or additional models could be used tocontrol the production equipment in the ammonia production system 100 oranother system. Although FIGS. 3A through 3I illustrate an example of auser interface for controlling an ammonia production system, any otheror additional user interface could be used. Also, the arrangement andcontent of the user interface 300 shown in FIGS. 3A through 3I is forillustration only.

FIG. 4 illustrates an example method 400 for controlling an ammoniaproduction system. The embodiment of the method 400 shown in FIG. 4 isfor illustration only. Other embodiments of the method 400 could be usedwithout departing from the scope of this disclosure. Also, for ease ofexplanation, the method 400 is described with respect to the APC system106 controlling the ammonia production system 100. The method 400 couldbe used by any device or system to control any suitable ammoniaproduction system.

Operating data for the ammonia plant is analyzed at step 402. This couldinclude, for example, the APC system 106 receiving data identifying howcertain controlled, manipulated, and disturbance variables are behavingduring normal operation of the ammonia production system 100. This couldalso include the APC system 106 receiving step-testing data associatedwith testing of the ammonia production system 100. The data could bestored in a database or other repository.

Models of an ammonia plant are generated at step 404. This couldinclude, for example, making adjustments to prior models based on thedata collected at step 402. This could also include generating newmodels based on the data collected at step 402.

Adjustments to the operation of the ammonia plant are made at step 406.This could include, for example, the APC system 106 adjusting theproduction equipment 102 using the new models. As particular examples,models could be used to control CV1, CV3, CV6, and CV7 using MV1-MV4, tocontrol CV2 using MV6 and optionally MV8, and to control CV8-CV10 usingMV9.

One or more control objectives and optimization objectives areimplemented at step 408. This could include, for example, controllingthe specified CVs using the specified MVs while taking into account bothcertain control objectives and optimization objectives. Among otherthings, these objectives may help to increase ammonia production in theammonia production system 100 while reducing fuel/energy consumption inthe ammonia production system 100.

Although FIG. 4 illustrates one example of a method 400 for controllingan ammonia production system, various changes may be made to FIG. 4. Forexample, while shown as a series of steps, various steps in FIG. 4 couldoverlap. Also, various steps in FIG. 4 could be repeated, such as whensteps 406-408 are routinely performed and steps 402-404 are repeated ata much longer interval. In addition, steps 402-404 could be performed byone device to generate or modify models of the system 100, and steps406-408 could be performed by another device (such as a controller)using the models of the system 100.

In some embodiments, various functions described above are implementedor supported by a computer program that is formed from computer readableprogram code and that is embodied in a computer readable medium. Thephrase “computer readable program code” includes any type of computercode, including source code, object code, and executable code. Thephrase “computer readable medium” includes any type of medium capable ofbeing accessed by a computer, such as read only memory (ROM), randomaccess memory (RAM), a hard disk drive, a compact disc (CD), a digitalvideo disc (DVD), or any other type of memory.

It may be advantageous to set forth definitions of certain words andphrases used throughout this patent document. The term “couple” and itsderivatives refer to any direct or indirect communication between two ormore elements, whether or not those elements are in physical contactwith one another. The terms “application” and “program” refer to one ormore computer programs, software components, sets of instructions,procedures, functions, objects, classes, instances, related data, or aportion thereof adapted for implementation in a suitable computer code(including source code, object code, or executable code). The terms“transmit,” “receive,” and “communicate,” as well as derivativesthereof, encompass both direct and indirect communication. The terms“include” and “comprise,” as well as derivatives thereof, mean inclusionwithout limitation. The term “or” is inclusive, meaning and/or. Thephrases “associated with” and “associated therewith,” as well asderivatives thereof, may mean to include, be included within,interconnect with, contain, be contained within, connect to or with,couple to or with, be communicable with, cooperate with, interleave,juxtapose, be proximate to, be bound to or with, have, have a propertyof, or the like. The term “controller” means any device, system, or partthereof that controls at least one operation. A controller may beimplemented in hardware, firmware, software, or some combination of atleast two of the same. The functionality associated with any particularcontroller may be centralized or distributed, whether locally orremotely.

While this disclosure has described certain embodiments and generallyassociated methods, alterations and permutations of these embodimentsand methods will be apparent to those skilled in the art. Accordingly,the above description of example embodiments does not define orconstrain this disclosure. Other changes, substitutions, and alterationsare also possible without departing from the spirit and scope of thisdisclosure, as defined by the following claims.

1. An apparatus comprising: at least one memory operable to store atleast one model, the at least one model associated with productionequipment operable to produce ammonia, the production equipmentcomprising a reformer section, a carbon dioxide wash section, and anammonia synthesis reactor section; and at least one processor operableto control the production equipment using the at least one model;wherein the at least one model is associated with a plurality ofcontrolled variables and a plurality of manipulated variables; whereinat least some of the controlled variables are associated with at leastone of: the reformer section, the carbon dioxide wash section, and theammonia synthesis reactor section; and wherein at least some of themanipulated variables are associated with at least one of: the reformersection, the carbon dioxide wash section, and the ammonia synthesisreactor section.
 2. The apparatus of claim 1, wherein: the reformersection includes a primary reformer and a secondary reformer; at leastone of the controlled variables is associated with at least one of:methane slip in the secondary reformer, an air compressor that isoperable to affect operation of the reformer section, and one or moreheating limits of the primary reformer; and at least one of themanipulated variables is associated with at least one of: a natural gasfeed flow, a steam flow or steam-to-gas ratio or steam-to-hydrocarbonratio in the primary reformer, an air flow or air-to-gas ratio in thesecondary reformer, and methane slip in the primary reformer.
 3. Theapparatus of claim 2, wherein the at least one processor is operable toat least one of: maintain the methane slip in the secondary reformerbetween specified limits; maintain the air compressor below an operatinglimit; and maintain the primary reformer below the one or more heatinglimits.
 4. The apparatus of claim 3, wherein the at least one processoris operable to at least one of: maximize throughput of the productionequipment; maintain the methane slip in the secondary reformer at ornear an optimum target to minimize natural gas consumption; and maintainthe methane slip in the primary reformer at or near an optimum target tominimize natural gas consumption.
 5. The apparatus of claim 1, whereinat least one of the controlled variables is associated with carbondioxide slip in the carbon dioxide wash section; and at least one of themanipulated variables is associated with at least one of: a flow rate ofa lean solution in the carbon dioxide wash section, and a temperature ofthe lean solution.
 6. The apparatus of claim 5, wherein the at least oneprocessor is operable to maintain the carbon dioxide slip in the carbondioxide wash section below a maximum limit.
 7. The apparatus of claim 6,wherein the at least one processor is operable to at least one of:minimize the carbon dioxide slip in the carbon dioxide wash section to alow limit; and minimize the flow rate of the lean solution to saveenergy.
 8. The apparatus of claim 1, wherein at least one of thecontrolled variables is associated with at least one of: a pressure of asynthesis reactor in the ammonia synthesis reactor section, and asynthesis gas compressor in the ammonia synthesis reactor section; andat least one of the manipulated variables is associated with a suctionpressure of the synthesis gas compressor.
 9. The apparatus of claim 8,wherein the at least one processor is operable to at least one of:maintain the pressure of the synthesis reactor below a maximum limit;and maintain the synthesis gas compressor below an operating limit. 10.The apparatus of claim 9, wherein the at least one processor is operableto maintain the suction pressure of the synthesis gas compressor at ornear an optimum target.
 11. The apparatus of claim 1, wherein the atleast one processor is operable to generate the at least one model. 12.A method comprising: storing at least one model, the at least one modelassociated with production equipment operable to produce ammonia, theproduction equipment comprising a reformer section, a carbon dioxidewash section, and an ammonia synthesis reactor section; and controllingthe production equipment using the at least one model; wherein the atleast one model is associated with a plurality of controlled variablesand a plurality of manipulated variables; wherein at least some of thecontrolled variables are associated with at least one of: the reformersection, the carbon dioxide wash section, and the ammonia synthesisreactor section; and wherein at least some of the manipulated variablesare associated with at least one of: the reformer section, the carbondioxide wash section, and the ammonia synthesis reactor section.
 13. Themethod of claim 12, wherein: the reformer section includes a primaryreformer and a secondary reformer; at least one of the controlledvariables is associated with at least one of: methane slip in thesecondary reformer, an air compressor that is operable to affectoperation of the reformer section, and one or more heating limits of theprimary reformer; and at least one of the manipulated variables isassociated with at least one of: a natural gas feed flow, a steam flowor steam-to-gas ratio or steam-to-hydrocarbon ratio in the primaryreformer, an air flow or air-to-gas ratio in the secondary reformer, andmethane slip in the primary reformer.
 14. The method of claim 13,further comprising at least one of: maintaining the methane slip in thesecondary reformer between specified limits; maintaining the aircompressor below an operating limit; and maintaining the primaryreformer below the one or more heating limits.
 15. The method of claim14, further comprising at least one of: maximizing throughput of theproduction equipment; maintaining the methane slip in the secondaryreformer at or near an optimum target to minimize natural gasconsumption; and maintaining the methane slip in the primary reformer ator near an optimum target to minimize natural gas consumption.
 16. Themethod of claim 12, wherein at least one of the controlled variables isassociated with carbon dioxide slip in the carbon dioxide wash section;and at least one of the manipulated variables is associated with atleast one of: a flow rate of a lean solution in the carbon dioxide washsection, and a temperature of the lean solution.
 17. The method of claim16, further comprising maintaining the carbon dioxide slip in the carbondioxide wash section below a maximum limit.
 18. The method of claim 17,further comprising at least one of: minimize the carbon dioxide slip inthe carbon dioxide wash section to a low limit; and minimize the flowrate of the lean solution to save energy.
 19. The method of claim 12,wherein at least one of the controlled variables is associated with atleast one of: a pressure of a synthesis reactor in the ammonia synthesisreactor section, and a synthesis gas compressor in the ammonia synthesisreactor section; and at least one of the manipulated variables isassociated with a suction pressure of the synthesis gas compressor. 20.The method of claim 19, further comprising at least one of: maintain thepressure of the synthesis reactor below a maximum limit; and maintainthe synthesis gas compressor below an operating limit.
 21. The method ofclaim 20, further comprising maintaining the suction pressure of thesynthesis gas compressor at or near an optimum target.
 22. The method ofclaim 12, further comprising generating the at least one model.
 23. Acomputer program embodied on a computer readable medium and operable tobe executed, the computer program comprising computer readable programcode for: storing at least one model, the at least one model associatedwith production equipment operable to produce ammonia, the productionequipment comprising a reformer section, a carbon dioxide wash section,and an ammonia synthesis reactor section; and controlling the productionequipment using the at least one model; wherein the at least one modelis associated with a plurality of controlled variables and a pluralityof manipulated variables; wherein at least some of the controlledvariables are associated with at least one of: the reformer section, thecarbon dioxide wash section, and the ammonia synthesis reactor section;and wherein at least some of the manipulated variables are associatedwith at least one of: the reformer section, the carbon dioxide washsection, and the ammonia synthesis reactor section.
 24. The computerprogram of claim 23, wherein: the reformer section includes a primaryreformer and a secondary reformer; at least one of the controlledvariables is associated with at least one of: methane slip in thesecondary reformer, an air compressor that is operable to affectoperation of the reformer section, and one or more heating limits of theprimary reformer; and at least one of the manipulated variables isassociated with at least one of: a natural gas feed flow, a steam flowor steam-to-gas ratio or steam-to-hydrocarbon ratio in the primaryreformer, an air flow or air-to-gas ratio in the secondary reformer, andmethane slip in the primary reformer.
 25. The computer program of claim23, wherein at least one of the controlled variables is associated withcarbon dioxide slip in the carbon dioxide wash section; and at least oneof the manipulated variables is associated with at least one of: a flowrate of a lean solution in the carbon dioxide wash section, and atemperature of the lean solution.
 26. The computer program of claim 23,wherein at least one of the controlled variables is associated with atleast one of: a pressure of a synthesis reactor in the ammonia synthesisreactor section, and a synthesis gas compressor in the ammonia synthesisreactor section; and at least one of the manipulated variables isassociated with a suction pressure of the synthesis gas compressor.